Cyclic adsorption process



July 16, 1957 Onginal Filed April 8, 1954 Fl6.l.

STRIPPED GAS OUT am as m E. B. MILLER r 2,799,362

cycuc ABSORPTION PROCESS 6 Sheets-Sheet 1 4: a 2 q a: q m 3 23 PM'-r--------, I 21 aauna L- Q. INVENTOR ERNEST BJIILLER ATTORNEYS July16, 1957 a B. MILLER 2,799,352

CYCLIC ADSORPTION PROCESS Original Filed April 8, 1954 v6 Sheets-Sheet 2FIG.2.

INVENFOR ERNEST B. MILLER ATTORNEYS y 1957 E. B. mLLER 2,799,362

CYCLIC ADSORPTION PROCESS Original Filed April 8, 1954 6 Sheets-Sheet 4INVENTOR ERNEST B. MILLER mfw ATTORNEYS July 16, 1 57 E. B. MILLER2,799,362

CYCLIC ADSORPTION PROCESS Original Filed April 8, 1954 6 Sheets-Sheet 5INVENTOR ERNEST B. MILLER ATTORNEYS J ly 16, 1957 E. B. MILLER 2,799,362

' CYCLIC ABSORPTION PROCESS 6 Sheets-Sheet 6 Original Filed April 8,1954 FIG. I.

\ FIG. lo.

INVENTORI ERNEST B. MILLER ATTORNEYS United States Patent 2,799,362CYCLIC ABSORPTION PROCESS Ernest B. Miller, Houston, Tex., assignor toJefferson Lake Sulphur Company, New Orleans, La., a corpora .tion of NewJersey Continuation of abandoned application Serial No. 421,746, April8, 1954. This application October 19, 1956, Serial No. 619,375

8 Claims. (Cl. 183-114.2)

This invention relates to gas dehydrating and has more particularreference to a novel and improved continuous method of removing moistureand condensable hydrocarbons from wet natural gas at the source, priorto the transmission thereof through pipe lines and recovering thecondensable hydrocarbons.

One object of the present invention is to provide a novel and improvedmethod of dehydrating wet gas using an adsorbent, such as silica gel,and recovering a large percentage of the condensable hydrocarbons, suchas gasoline, etc.

Another object of the present invention is to provide a novel method ofrecovering condensable hydrocarbons from wet natural gas, which ischaracterized by maintaining at least one bed of adsorbent material ineach of a plurality of zones; continuously heating and recycling anactivating gas through at least one of said zones to vaporize themoisture and condensable hydrocarbons contained in the adsorbentmaterial therein and reactivate the adsorbent material; continuouslydirecting the flow of a cooling medium through at least another one ofsaid zones to cool the adsorbent material therein; continuouslydirecting the flow of the wet natural gas through the remainder of saidzones so that the contained moisture and condensablehydrocarbons will beadsorbed by the adsorbent material therein; periodically shifting therelative position of the particular adsorbent beds and the particularflow 'of fluids in each of said zones so that each zone becomes, insuccession, a reactivation zone, a cooling zone, and an adsorption zone;continuously directing the flow of the recycling activation gas, afterits passage through the reactivation zone, through a condensing andseparating zone, and there condensing and recovering the water andcondensable hydrocarbons and continuously directing the flow of thestripped gas back into the recycling path.

Another object of the present invention is to provide a novel method ofdehydrating wet natural gas, as characterized above, wherein acontinuous flow of a purging medium is directed through at least anotherone of said zones to purge the zone by removing all remaining activationgas and any remaining moisture and condensable hydrocarbons deposited onthe adsorbent material, thereby purging the zone, and wherein thepurging gas, after its passage through the purging zone or zones, isdirected into the flow of the gas being treated.

A further object of the present invention is to provide a novel method,as characterized above, wherein the gas being treated is dehydrated intwo or more stages, and wherein the last dehydrating passage of the gasbeing treated is made through freshly activated adsorbent material.

Other objects and advantages of the invention will appear in thefollowing specification when considered in connection with theaccompanying drawings, in which:

Fig. 1 is a schematic view showing the arrangement of the embodiment ofapparatus employed in carrying out ice the method of the presentinvention and the flow of the various fluids therethrough;

Fig. 2 is a side elevational view of the dehydrater shown in'Fig. l;

Fig. 3 is a plan view of the apparatus shown in Fig. 2;

Fig. 4 is a vertical sectional view taken on the line 44 of Fig. 3, butomitting the driving apparatus;

Fig. 5 is a horizontal sectional view taken on the line 55 of Fig. 4;

Fig. 6 is a fragmentary sectional view taken on the line 6--6 of Fig. 4,showing the manner ofbracing the upper ends of the elongated fluidtreating material containing vessels;

Fig. 7 is a fragmentary sectional view taken on the line 77 of Fig. 4,showing the manner of supporting the lower ends of the elongated fluidtreating material containing vessels;

Fig. 8 is a horizontal sectional view taken on the line 88 of Fig. 4; 1

Fig. 9 is a detail sectional view taken on the line 9-9 of Fig. 8;

Fig. 10 is a vertical sectional view, with parts broken away, of thefluid treating material containing vessels shown in Fig. 4, showing thecontainers for holding the treating material mounted therein; and

Fig. 11 is a plan View of the container shown in Fig. 10.

This application is a continuation of my co-pending application SerialNo. 421,746, filed April 8, 1954, now abandoned, for Cyclic AdsorptionProcess.

The present invention is drawn to a novel method of dehydrating wetnatural gas under high pressure and removing the condensablehydrocarbons therefrom, and is an improvement over the method disclosedand claimed in my co-pending application Serial No. 406,312, filedJanuary 26, 1954, now Patent No. 2,739,670, issued March 27, 1956, forCyclic Adsorption Process.

Referring now to the drawings, there is shown, in Fig. 1, one embodimentof apparatus and the arrangement thereof for carrying out the method ofthe present invention. The apparatus shown includes a seven-stagedehydrater 1, the first, second and third stages of which are employedto dehydrate the wet gas, the fourth stage is employed to cool theadsorbent material within the dehydrater, the fifth stage is employed topurge the adsorbent material in the dehydrater, the sixth stage isemployed to reactivate the adsorbent material, and the seventh stage isemployed as a second purging stage; an intercooler 2 is employed to coolthe wet gas between the cooling and third dehydration stages; a heater 3employed to heat the gas used in the reactivation stage of thedehydrater; a fan or blower 4 for recirculating the activation gasthrough the reactivation stage of the dehydrater; and a condenserseparator 5 employed to condense the moisture and condensablehydrocarbons contained in the recirculating activation gas after it haspassed through the reactivation stage of the dehydrater.

The wet gas being treated is delivered, at high pressure, from the usualcompressor or source of supply (not shown), to the first stage of thedehydrater by means of a pipe line 6. The gas passes through the firstdehydration stage of the dehydrater, where some of the moisture andcondensable hydrocarbons are removed. From the first dehydration stageof the dehydrater the gas passes through pipe line 7 to the seconddehydration stage of the dehydrater. After passing through the seconddehydration stage of the dehydrater, where additional moisture andcondensable hydrocarbons are removed, the gas passes through pipe line 8to the third dehydration stage of the dehydrater. After passing throughthe third dehydration stage of the dehydrater, the moisture andhydrocarbon stripped gas passes through pipe line 9 into the intercooler2, where its temperature is reduced to from about 80 F. to 100 F. Fromthe intercooler 2, the cool stripped gas passes through pipe line to thecooling stage of the dehydrater where it cools the adsorbent material inthe cooling stage. From the cooling stage the stripped gas passesthrough pipe line 11 to its various points of use.

The captive activation gas is heated in the heater 3 to a temperature offrom 300 F. to 600 F., depending upon the moisture content and the typeof hydrocarbons to be recovered, and from the heater passes through apipe line 12 into the reactivation stage of the dehydrater. The heatedgas passes downwardly through the reactivation stage, vaporizing andstripping the accumulated moisture and hydrocarbons from the adsorbent.The heated gas and the vapors stripped from the adsorbent pass through apipe line 13 to the condenser separator 5, where the moisture andcondensable hydrocarbons are condensed and separated. The water andhydrocarbons are drained from the bottom of the separator by means of asuitable drain line.

From the condenser separator 5 the now stripped gas passes through apipe line 14 to the fan or blower 4 and is recirculated by the blowerthrough a pipe line 15 and the heater 3 back through the activationstage of the dehydrater. This recirculation process is continuous.

The captive stream of gas in the activation system is circulated bymeans of the blower 4, through the heater 3, the activation stage of thedehydrater, and the condenser separator 5. The composition of thisstream will build up gradually in terms of condensable vapors, composedchiefly of hydrocarbons, until the dew point of the captive gas streamreaches condenser temperature, and will, thereafter, yield as liquidsall the condensable vapors desorbed in the reactivation stage of thedehydrater.

The gas used as the first purging medium may be taken from the pipe line11 through pipe line 16 and passes downwardly through the first purgingstage of the dehydrater. As the purging gas passes through the firstpurging stage it purges the adsorbent material therein by removing allremaining activating gas and any remaining moisture and condensablehydrocarbons contained in the adsorbent material. From the first purgingstage, the purging gas passes through pipe line 17 into pipe line 14 andto the blower 4 and joins the recycling activation gas.

A portion of the gas flowing to the heater 3 through pipe line 15 isdiverted through pipe line 18 to the second purging stage, and afterpassing through the second purging stage, passes through pipe line 19into pipe line 6 to be joined with the flow of the gas being treated onits way to the dehydrater.

While any suitable type of dehydrator may be employed to practice themethod of the present invention, the dehydrater illustrated is generallysimilar to the fluid treating apparatus shown in my co-pendingapplication, Ser. No. 406,310, filed January 26, 1954, now Patent No.2,751,033 dated June 19, 1956, for Fluid Treating Apparatus.

As shown in Figs. 2 to 11, inclusive, the dehydrater comprises anelongated upright cylindrical pressure vessel 21) having flangedvertically aligned circular openings 21, 22 in its top and bottom walls,respectively, closed by top and bottom flanged cover plates 23, 24,removably secured to cover said openings, as by bolting; suitableframework, indicated at 25, for supporting the vessel in an uprightposition; a rotatable vertical shaft 26 extending through the pressurevessel 20 with its upper end journaled in a suitable cap bearing carriedby the upper closure member 23 and with its lower end extending througha suitable shaft seal, secured to the bottom of the lower closure member24; a vertical shaft 27 coupled to the bottom end of the shaft 26 andconnected to suitable diiferential gearing, indicated at 28, driven by amotor 29; a support disc 30 fixedly mounted on the shaft 26 for rotationtherewith within said pressure vessel and providing support for aplurality of elongated fluid treating material containing cylindricalvessels 31; upper and lower distributive assemblages, indicatedgenerally at 32, 33, each assemblage comprising an annular stationarymember 34 having a plurality of compartments or manifolds formedtherein, a tube sheet disc valve 35 slidably mounted on the shaft 26 forrotation therewith, a spring support disc 36 fixedly mounted on theshaft 26 and supporting a plurality of coiled springs 37 which engagethe tube sheet disc valve 35 and tightly press it against the open endof the annular stationary member 34; a plurality of flexible pipes 38,each connecting the upper end portion of one of the vessels 31 and thetube sheet disc valve 35 of the upper distributive assemblage; aplurality of flexible pipes 39, each connecting the lower end portion ofone of the vessels 31 and the tube sheet disc valve 35 of the lowerdistributive assemblage, a plurality of inlet-outlet conduits, sevensuch being shown, 40, 41, 42, 43, 44, and 46, connected to the annularstationary member 34 of the upper distributive assemblage and extendingupwardly through the upper cap closure member 23, for the ingress andegress of fluids to and from the upper stationary member 34; and aplurality of inlet-outlet conduits, seven such being shown, 41), 41',42', 43', 44', 45, 46, connected to the annular stationary member 34 ofthe lower distributive assemblage and extending downwardly through thelower cap closure member 24 for the ingress and egress of fluids to andfrom the lower stationary member 34.

The cylindrical pressure vessel 20 and the cap cover members 23, 24 arepreferably made of heavy boiler plate. The flanges formed on theperipheries of the openings 21, 22 of the vessel 26 and the peripheriesof the cap cover members 23, 24 are preferably formed of heavy ironrings, rectangular in cross section and are welded to the peripheraledges of the openings and the cover plates, as indicated at 47.

The shafting 26, preferably and as shown, is formed of three sections,an upper section 48, an intermediate section 49, and a lower or bottomsection 50. The upper and lower sections 48 and 50 consist of solid rod,round in cross section. The intermediate section 49 consists of a hollowpipe having an internal diameter considerably larger than the diametersof the upper and lower sections.

The upper section 38 has its upper end journaled in a suitable capbearing 51 carried by the upper cover member 23 and its lower endsupported in a support bushing 52 mounted in the upper end of theintermediate section 49 with a pin 53 passing through the two sectionsand the bushing for rigidly and detachably securing the two sectionstogether.

The bottom section 50 has its upper end engaged in a support bushing 54mounted in the lower end of the intermediate section 49 with a pin 55passing through the two sections and the bushing for rigidly anddetachably securing the two sections together, and with its lower endextending through the lower cover member 24 and a suitable shaft seal 56and coupled to the upper end of theshaft 27.

The support disc 30 which supports the cylindrical vessels 31 iscomposed of two semi-annular fiat pieces 57, the inner adjacent straightedges of which are provided with flanges which are bolted together toform the complete disc. This is to permit of assembling the disc withinthe pressure vessel 20.

The disc 30 (see Figs. 4 and 7) is fixedly secured, as by bolting, to acollar 58 fixedly secured to the intermediate section 49 of the shaft26, so that the disc will rotate with the shaft. The outer peripheraledge portion of the disc 30 is supported by means of a plurality ofsupporting links or arms 59, each having its upper end bolted to one ofa plurality of circumferentially spaced lugs 60 carried by a collar 61fixedly secured to the intermediate section 49 of the shaft 26 and itslower end bolted to one of a plurality of circumferentially spacedupstanding lugs 62 secured to the upper surface of the disc 30.

The vessels 31 are supported by the disc 30, as by means of a pluralityof supporting links or arms 63 in the form of short sections ofstructural angles, each arm 63 having its outer end portion fixedlysecured to the bottom and one side of one of said vessels 31, as bywelding, and its inner end portion fixedly secured, as by bolting, toone of a plurality of circumferentially spaced dependent lugs 64, in theform of short sections of I-beams, welded to the upper surface of thedisc (see Figs. 4 and 7). 1

Means may be provided for holding the cylindrical vessels 31 in theirupright position encircling the shaft 26. In the particular embodimentof the apparatus illustrated, such means are shown as comprising a disc65 composed of two semi-annular flat pieces 66, 66, the inner adjacentstraight edges of which are provided with flanges which are boltedtogether to form the complete disc. This is to permit of assembling thedisc within the pressure vessel 20. The disc 65 (see Figs. 4 and 6) isfixedly secured, as by bolting, to a collar 67 fixedly secured to theintermediate section 49 of the shaft 26, so that the disc will rotatewith the shaft. The upper end portions of the vessels 31 are held intheir upright position by the disc 65, as by means of a plurality ofbracing strips or arms 68 in the form of short sections of structuralangles. Each arm 68 has its outer end bolted to a lug 69 welded on theouter surface of one of the vessels 31 and its inner end portion fixedlysecured, as by bolting, to the upper surface of the disc 65.

The upper and lower distributive assemblages 32, 33 are identical inconstruction and, as shown in Fig. 4, each comprises an annulartrough-shaped stationary member 34 having a plurality of compartments ormanifolds formed therein; a tube sheet disc valve 35 slidably mounted onthe shaft 26 for rotation therewith; and a spring support disc 36fixedly mounted on the shaft 26 and supporting a plurality of coiledsprings 37 which engage the tube sheet disc valve 35 and tightly pressit against the open end of the annular stationary member 34.

The upper and lower annular stationary members 34 are identical inconstruction and, as shown in Figs. 4, 5, 8 and 9, each is formed in theshape of an annular trough having an annular top (or bottom) wall 70 andannular side walls 71, 72 (see Figs. 4 and 9).

The member 34 is divided into a plurality of compartments or manifolds,as by means of a plurality of circumferentially spaced pairs of wallmembers 73 extending transversely of the member 34 and having their top(or bottom) and side walls welded to the top (bottom) and side walls ofthe member 34 to form gas-tight joints. Seven such compartments ormanifolds are shown and, for the purposes of clairity of description,designated manifolds a, C, in and g, p i ly The upper member 34 of theupper distributive assemblage 32 is held stationary relative to therotation of the shaft 26 and the upper tube sheet disc valve 35 by theupper inlet-outlet conduits 40, 41, 42, 43, 44, 45 and 46, which areWelded to the upper cap closure member 23 and have their lower endsconnected, as by welding, to the manifolds a, b, c, d, e, f and g,therewith.

The lower member 34 of the lower distributive assemblage is heldstationary relative to the rotation of the shaft 26 and the lower tubesheet disc valve 35 by the lower inlet-outlet conduits 40, 41, 42', 43,44, 45', and 46, which are welded to the lower cap closure 24 and havetheir upper ends connected, as by welding, to the manifolds f d g,respectively,

in the lower member 34 to provlde communication therewith.

The upper and lower tube sheet disc valves 35 are identical inconstruction and, as shown in Fig. 4, each comprises a flat metal dischaving a plurality of c'ircumferentially spaced circular openings 74formed in a circular row adjacent its periphery. The disc is providedwith a collar '75 having a plurality of radially extending reinforcingribs welded to its bottom surface or cast integral therewith. The collar75 is keyed on the upper (lower) section of the shaft 26 to havelongitudinal movement therealong as well as rotative movement therewith,as by means of a set screw '76 slidably engaging in a Y longitudinalgroove 7'7 formed in the upper (lower) section of the shaft 26. A secondcollar 78 is fixedly secured to the shaft 26 immediately beneath thecollar 75 to limit the inward movement of the disc as it moveslongitudinally of the shaft 26. The disc 35, as well as the collar 75,are loosely'fitted on the shaft 26 so that the disc valve can be movedslightly to conform to any change in the plane of the engaged surface ofthe stationary member 34, due to unequal expansion and contraction.

The tube sheet disc 35 is so mounted on the shaft 26 that it slidablyengages the open bottom (top) end of the annular stationary member 34with the circular row of openings 74 vertically aligned with themanifolds a, b, c, d, e, f and g, so that each manifold will be incommunication with a group of the circular openings.

The upper and lower spring support discs 36 are identical inconstruction and, as shown in Fig. 4, each comprises a metal discmountedon the shaft and having a hub '79 provided with a plurality ofcircumferentially spaced radial ribs or webs welded to the under face ofthe disc to strengthen it. The hub is fixedly secured to the shaft, asby a set screw. A plurality of vertically extending circumferentiallyspaced coiled springs 37 are interposed between the tube sheet discvalve 35 and the spring support disc 36. In order to insure that thesprings 37 remain in proper position, they are mounted on and betweenshort stubs 80 extending upwardly from the disc 36 and shortcorresponding stubs 80' extending downwardly from the disc 35. Theconstruction and arrangement is such that the springs 37 will keep thedisc valve 35 evenly and firmly pressed into engagement with the undersurface of the annular stationary member 34.

The upper and lower flexible pipes 38, 39, which connect the upper andlower end portions of the fluid treating material containing vessels 31to the upper and lower distributive assemblages are identical inconstruction and, as shown in Figs. 4 and 10, each comprises a thinwalled cylindrical metal tube having the greater portion of its wallformed in a sinuous shape to give it flexibility, the outer cylindricalend of each tube is detachably secured to a nozzle 81 formed on theupper (lower) end portion of the vessel 31, as by strapping. Thecylindrical inner end of the tube is provided with an integral flange82. The opening in the cylindrical inner end of the tube is aligned withone of the circular openings 74 formed in the upper (lower) tube sheetdisc valve 35 and the flange 82 is detachably secured to the outersurface of the disc valve, as by countersunk bolts, so that the innersurface of the disc wall will be smooth and uninterrupted (see Fig. 4),

To prevent the escape of gas between the rotating tube sheet disc valve35 and the manifolds in the member 34, sealing ring gaskets 83 areplaced at the juncture of the side walls of the member 34 and the discvalve 35. The ring gaskets 83 are wedged into annular troughs 84,secured, as by welding, to the outer surface of the side walls of themember 34. Each trough comprises an annular top (bottom) wall 35 and anannular side wall 86. The ring gaskets 83, preferably and as shown,comprise a plurality of annular strips of packing, generally rectangularin cross section and made of any suitable material, such as Teflon orsicila impregnated asbestos.

7 are sealed ofi from each other by means of cross seals 87, each sealedinto a recess 88 formed by the adjacent end walls of the manifolds and abottom plate 89 vertically space from the open end of the manifolds (seeFigs. 8 and 9). Each cross seal is tightly wedged in its recess with itsouter ends in tight engagement with the adjacent side walls of theannular seals 83 and with its bottom surface in sealing engagement withthe upper (lower) surface of the tube sheet disc. In order for the outerends of the cross seals to engage the adjacent side walls of the annularseals 83, the portions of the side walls 71 and '72 of the member 34which extend between each pair of adjacent transverse members 73 are cutaway, as indicated at 90, for a distance equal to the thickness of theseals 83 (see Fig. 9).

The widths of the manifolds a, b, c, d, e, f and g are substantially thesame as the internal diameters of the circular openings 74 in the tubesheet disc 35, and each of the cross seals 87 is of a width greater thanthe circular openings 74 so that each cross seal can etfectively sealoff one of the openings.

Each of the openings 74 formed in the upper tube sheet disc 35 is inverticalalignment with a corresponding one of the openings 74 formed inthe lower tube sheet disc 35 and each of the cross seals 87 whichseparate the manifolds a, b, c, d, e, and g formed in the upperstationary member 34 is in vertical alignment with a corresponding oneof the cross seals 87 which separate thg manifolds a, b, c, d, e, if,and g formed'in the lower stationary member 34.

When the rotary disc valves 35 are stationary, the foregoingarrangement, in effect, divides the fluid treating material containingvessels 31 into seven stages or groups, with one group connected tocommunicate with the manifolds a, one group connected to communicatewith the manifolds b, one group connected to communicate with themanifolds c, one group connected to communicate with the manifolds d,one group connected to communicate with the manifolds e, one groupconnected to communicate with the manifolds f, and one group connectedto communicate with the manifolds g, so that seven separate, distinctand continuous flows of fluid may pass through the apparatus. Each flowentering the upper distributive assemblage by means of one of theinlet-outlet conduits 40, 4-1, 42, 43, 44, 45, and 46, thence throughone of the groups or stages of vessels 31 into the lower distributiveassemblage and out through one of the inletoutlet conduits 40, 41, 42,43', 44, 45', or 46'. As the upper and lower disc valves rotate, each ofthe flows of fluid will successively pass through the vessels 31.

The silica gel containing vessels 31 are identical in construction and,as shown in Figs. 10 and I1, each comprises an elongated hollow tubularmember 91 having a closed bottom end and an open upper end provided witha flanged collar 92 to which is secured, as by bolting, a removablecover plate 93.

A horizontally disposed annular disc 94 is mounted in the lower endportion of the member 91 and is secured therein, as by welding, to forma gas-tight joint between the outer peripheral edge of the disc and theside wall of the member 91. The lower annular disc 94 forms a supportfor an elongated annular fluid treating material container 95. Thecontainer 95 is removably mounted within the member 91, with its bottomend resting on the annular disc 94 and with the longitudinal open end ofthe container aligned with the opening in the disc.

The tubular member 91 has a tapered side wall for a purpose hereinafterto be described and is provided with upper and lower circular openings96 in which are secured, as by welding, the nozzles 81 to which theupper and lower flexible pipes 38 and 39 are secured.

A baffle member 97 is mounted in the space between the bottom of themember 91 and the annular disc 94, and an upper baflie member 98 issecured to the underside of the cover plate 93 and is removabletherewith.

The upper and lower baffie members 97 and 98 are identical inconstruction and, as shown in Fig. 10, each comprises a generallyelliptical-shaped flat sheet 99 extending upwardly (downwardly) from thebottom (top) of the member 91 to insure an even flow of fluid throughthe member 91; a side wall forming member 100; and insulating material101 placed within the pocket formed by the members 99 and 100 and thebottom (top) wall of the member 91 (see Fig. 10).

The containers 95 are identical in construction and, as shown in Figs.10 and 11, each comprises two concentric tubular screens 102, 103, heldin spaced-apart relation by a plurality of longitudinal radial fins 104,with the annular space between the screens closed at the bottom, as by aflanged annular plate 105. The mesh of the screens is such as to retaina granular adsorbent material 106 in the annular space between thescreens. In the instant case, the adsorbent material may be of anyadsorbent having characteristics substantially like silica gel or thegel of other activated hydrous oxides. Preferably, silica gel is used.

Each of the containers 95 is closed at its top by means of concentrichoops or metal bands 107, 108 mounted on the concentric screens 102,.103, and a cover plate 109 detachably connected to the inner hoop orband 108, as by screws, and having a depending annular flange 110fitting between the hoops or bands 107, 108. A depending cylindrical fin111 is secured to the flange 110 and projects downwardly between andbelow the hoops or bands 107, 108, and fits in slits 112 formed in theupper ends of the radial fins 104, all as shown in Figs. 10 and 11. Theconstruction is such that, as the silica gel settles down, leaving aspace between the top portion of the wire screens devoid of silica gel,the fins 111 will prevent fluid from passing through the space.

Mounted within the inner wire screen 103 is an inverted substantiallyconically shaped baffle member 113. The baflle member 113 is closed atits apex which extends downwardly to a point near the bottom of thecontainer and has its upper peripheral edge suitably secured to the band108, as by welding. Preferably, the baffle member 113 is made of thinsheet metal.

When the container 95 is mounted within the hollow member 91, as shownin Fig. 10, the elongated annular space between the walls of the member91 and the inverted conical baffle member 113 forms an elongatedfrusto-conically shaped duct which is annular in cross section. Theannular container, filled with silica gel, is positioned in the ductbetween the members 91 and 113 in such manner that it forms a barrierextending longitudinally across the duct from top to bottom. The crosssectional areas of the duct at its top and bottom are substantiallyequal and the tapers of its side walls are such that a substantiallyuniform velocity is obtained on both sides of the barrier as fluid istransferred from the upstream to the downstream side, regardless of thedirection of flow, thereby creating a substantially constant static headover the face of the barrier, resulting in a substantially uniformdistribution of the fluid throughout the entire barrier area. Thus, itwill be seen that by using the members 91 and 113 as bafiie members, theentire area is made use of with resultant increase in efficiency,capacity and economy.

Means may be provided so that the containers 95 which hold the adsorbentmaterial may readily be removed from and replaced in the vessels 31. Asshown, such means may comprise an opening 11 formed in the top of thevessel 20 having a cylindrical member 115 welded therein and providedwith a readily removable closure disc 116 secured in the upper end ofthe member 115, as by means of a split shear ring 117 bolted thereto andfitted into a circumferential recess 113 formed in the inner surface ofthe member 115, and an O-ring packing 119 mounted between the closuredisc 116 and the side wall of the member 115 to insure gas tightness.

The flows of the various gases through the various 'the tube sheet discvalve 35 lower end portion of the group of vessels 31 which are stagesof the dehydrater and the auxiliary apparatus are schematically shown inFig. 1.

As there shown, the wet natural gas from which moisture and condensablehydrocarbons are to be removed, is supplied under high pressure by pipeline 6 and enters manifold a of the upper distributive assemblagethrough inlet-outlet conduit 40. From manifold a the gas passes throughopenings 74 formed in the upper tube sheet disc valve 35 and flexiblepipes 38 into the upper end portion of the group of vessels which are atthat time in communication with the manifold a. The gas passes downthrough the silica gel beds therein into the bottoms-of the vessels. Thebafiie members 113, in cooperation with the tapered side walls of thevessels 31, insure a substantially uniform flow and distribution of thewet gas through the silica gel beds, which adsorb some of the moisturecontent from the gas. From the bottoms of the vessels 31, the nowpartially dried gas passes through outlet pipes 39 and openings 74 inthe lower tube sheet disc valve 35 into the manifold a of the lowerdistributive assemblage.

From the lower manifold a of the lower distributive assemblage, the gaspasses through inlet-outlet conduit 40' and pipe line 7 to the seconddehydration stage and enters manifold b of the lower distributiveassemblage through inlet-outlet conduit 41. From the lower manifold bthe gas passes through openings 74 in the tube sheet disc valve 35 andinlet pipes 39 into the lower end portions of the group of vessels 31which are at that time in communication with manifold 11. The gas passesupwardly through the vessels 31 of the second group and through thesilica gel beds therein into the tops thereof, additional moisture andcondensable hydrocarbons being absorbed from the gas during its passagethrough the silica gel beds.

From the tops of the vessels 31 of the second adsorption group, the gaspasses through pipes 38 and openings 74 in the upper tube sheetdiscvalve of the upper distributive assemblage into the upper manifold12.

From the upper manifold b the gas passes through inlet-outlet pipe 41and pipe line 8 to the third adsorption stage and enters upper manifoldc of the upper distributive assemblage through inlet-outlet conduit 42.

From the upper manifold c the gas passes through openings 74 in the tubesheet disc valve 35 and inlet pipes 38 into the upper end portions ofthe group of vessels .31 which are at that time in communication withmanifold c. The gas passes downwardly through the vessels 31 of thethird group and through the silica gel beds therein into the bottomsthereof. The remaining moisture content of the gas being adsorbed duringits passage through the silica gel beds.

From the bottoms of the vessels 31 of the third group, the gas passesthrough pipes 39 and openings 74 inthe the tube sheet disc valve 35 intothe lower manifold c. From the lower manifold c the gas passes throughinletoutlet conduit 42' and pipe line 9 into an intercooler 2,

where it is cooled. The intercooler may be of the water circulatingtype. From the intercooler, the gas passes through pipe line 10 andinlet-outlet conduit 43 into manifold d of the lower distributiveassemblage. From the manifold d the gas passes through openings 74 inand inlet pipe 39 into the at that time in communication with manifoldd. The gas passes upwardly through the vessels 31 of the fourth groupand through the silica gel beds therein into the bottom thereof. Thecool, dry gas cools the silica gel beds in the fourth cooling stageduring its passage through the beds.

From the tops of the vessels '31 of the fourth group,

the now dried gas passes through oultet pipes 38 and outlet conduit 43and pipe line 11 to the various points of use.

The removal and recovery of the moisture and hydrocarbons from the bedsof adsorbent material is effected in the activation stage. Theactivation gas, a captive gas, is heated in a heater 3, where itstemperature is raised to from 300 F. to 600 F., depending upon themoisture content and the type of hydrocarbons to be recovered. From theheater, the heated activation gas passes through pipe line 12' andinlet-outlet conduit 45 into the upper manifold f of the upperdistributive assemblage. From the manifold f the hot activation gaspasses through openings 74 in the lower tube sheet disc valve 35 andflexible pipes 38 into the upper end portions of the groups of vessels31 which are at that time in communication with manifold f. The gaspasses downwardly through the vessels 31 of the activation group andthrough the silica gel beds therein into the bottoms thereof. As the hotgas passes through the adsorbent material it removes the moisture andhydrocarbons therefrom. From the bottoms of the vessels 31 the hot,moisture-hydrocarbon laden gas passes through flexible pipes 39 andopenings 74 in the lower tube sheet disc valve 35 into the lowermanifold j. From the lower manifold f, the hot gas passes throughinlet-outlet conduits 45 and pipe line 13 into a condenser-separator 5,where the moisture and condensable hydrocarbons are condensed andseparated. The water and hydrocarbons are drained from the bottom of theseparator by means of a suitable drain line.

From the condenser-separator the now stripped captive gas passes througha pipe line 14 to a fan or blower 4 and is recirculated by the blowerthrough pipe line 15 and the heater 3 back through the activation stage.This recirculation process is continuous.

The captive stream of gas in the activation system is circulated bymeans of the blower 4, through the heater 3, the activation stage of theapparatus, and the condenserseparator 5. The composition of this streamwill build up gradually in terms of condensable vapors, composed chieflyof hydrocarbons, until the dew point of the captive gas stream reachescondenser temperature, and will thereafter yield as liquid all thecondensable vapors desorbed in the reactivation stage of the apparatus.

In order to prevent slippage of the activation gas, rich inhydrocarbons, into the outgoing stripped gas and, at the same time,return the raw gas contained in the vessels 31 as they enter theactivation stage, .back to the raw gas stream, it is advisable toprovide a purging stage both ahead of and following the activationstage.

While any suitable gas may be used as the purging medium, preferably,and as shown, the gas used for the first purging stage is providedbydiverting a portion of the effluent dry natural gas from the coolingstage of the apparatus through pipe line 16 and inlet-outlet conduits 44into the upper manifold e of the upper distributive assemblage. From themanifold e the purging gas passes through openings 74 in the upper tubesheet disc valve 35 and flexible pipes 38 into the upper end portions ofthe group of vessels 31 which are at that time in communication withmanifold e. The gas passes downwardly through the vessels 31 of thefirst purging group and through the silica gel beds therein into thebottoms thereof. As the purging gas passes through the adsorbentmaterial it removes any remaining activation gas or deposited vaporstherefrom, thereby purging the beds. From the bottoms of the vessels 31,the purging gas passes through flexible pipes 39 and openings 74 in thelower tube sheet disc valve 35 into the lower manifold e. From the lowermanifold e the purging gas passes through inlet-outlet conduit 44' andpipe line 17 back into pipe line 14 and joins the recycling activationgas.

A portion of the recycling activation gas is diverted from pipe line 15for use as the purging gas in the second purging stage and passesthrough pipe line 18 and inletoutlet conduit 46 into the upper manifoldg of the upper distributive assemblage. From the manifold g the purginggas passes through openings 74 in the upper tube sheet disc valve 35 andflexible pipes 38 into the upper portions of the group of vessels 31which are at that time in communication with manifold g. The gas passesdownwardly through the vessels 31 of the second purging stage andthrough the silica gel beds therein into the bottoms thereof. As thepurging gas passes through the adsorbent material it removes the rawgas, thereby purging the beds. From the bottoms of the vessels 31 theeflluent gas passes through flexible pipes 39 and openings 74 in thelower tube sheet disc valve 35 into the lower manifold g. From the lowermanifold g the gas passes through inlet-outlet conduit 46 and pipe line19 back into pipe line 6 and joins the raw gas on its way to thedehydrater.

The gas being dehydrated makes three passages through the groups of thesilica gel containing vessels, while the reactivating medium, each ofthe purging mediums, and the cooling medium each make a single passagethrough a group of the silica gel containing vessels. For convenience indescription, the vessels which form the group through which the firstdehydration passage is made is called the first dehydration stage, thegroup through which the second dehydrating passage is made is calledthe-sec-' ond dehydration stage, the group through which the thirdpassage is made is called the third dehydration stage, the group throughwhich the cooling medium passes is called the cooling stage, the groupthrough which the hot gas used for reactivation passes is called thereactivation stage, the group through which the first purging mediumpasses is called the first purging stage, and the group through whichthe second purging medium passes is called the second purging stage.Also, the vessels 31 are called zones in which either dehydration,reactivation, cooling, or purging, takes place, depending upon theparticular fluid flowing therethrough at a given time. In addition, thecondenser separator is called a condensing and separating zone or stage.

In the particular embodiment of the invention illustrated the valvediscs 35 are rotated clockwise, as viewed in Fig. 8, and at the rate of1 revolution every minutes; thus, it will be seen that, as the valvesrotate, each of the vessels 31 will be successively brought intocommunication with the manifolds g, f, e, d, c, b and a in the upper andlower distributive assemblages, so that each vessel 31 will, in turn,become a second purging zone, an activation zone, a first purging zone,a cooling zone, a third dehydration zone, a second dehydration zone, anda first dehydration zone.

Suitable stop valves are provided at any desired point in any pipe lineto provide means for controlling the flow of the various mediums throughthe various stages of the dehydrater.

It is sometimes desirable to introduce an inert gas into the captiveactivation stream so that the inert gas may take the place of the gasmixture that otherwise would be present and thus avoid the liquefactionof methane, ethane, etc., that would condense along with the desiredhydrocarbons. For this purpose, a pipe line 12th having a stop valvetherein has been shown as connected to pipe line 15, the pipe line 120being connected to a suitable source of inert gas under suitablepressure.

From the foregoing, it readily will be seen that there has been provideda novel and improved method of removing and recovering moisture andcondensable hydrocarbons from wet natural gas, an improved method whicheliminates slippage of the activation gas into the outgoing stripped gasand returns the raw gas contained in the tubes 31 as they enter theactivation stage, back to the raw gas stream on its way to thedehydrator, an improved method that provides for removing the residualheat re maining in the adsorbent after the activation of the same,thereby increasing the efficiency of the operation.

While some of the flows of fluid through the apparatus have beendescribed as entering the top distributive assemblage and flowingdownward to and out of the bottom distributive assemblage, obviously,the flows may be in either direction.

Obviously, too, the present invention is not restricted to theparticular embodiment thereof herein shown and described. Moreover, itis not indispensable that all of the features of the invention be usedconjointly, since they may be advantageously employed in variouscombinations and sub-combinations.

What is claimed is:

1. In the removal of water vapor and condensable hydrocarbons from wetnatural gas involving the contact of adsorbent material with the gaswith resultant adsorption of the water vapor and condensablehydrocarbons by the adsorbent material and the subsequent treatment ofthe adsorbent material with a heated medium to vaporize and remove thewater and condensable hydrocarbons and thereby reactivate the absorbentmaterial for further contact with the natural gas, the improvement whichcomprises maintaining at least one bed of adsorbent material in each ofa plurality of zones; continuously heating and recycling a flow ofcaptive gas through at least one of said zones to vaporize the Water andcondensable hydrocarbons contained in the adsorbent material therein andreactive the adsorbent material; continuously directing the flow of apurging medium through at least another one of said zones to purge theadsorbent material therein by removing all of the remaining activationgas, moisture and condensable hydrocarbons therefrom; directing acontinuous flow of the raw natural gas so that it will make a firstpassage through at least an additional one of said zones and a secondpassage through the remainder of said zones so that the water vapor andsome of the condensable hydrocarbon content of the gas will be adsorbedby the adsorbent material therein; continuously cooling the raw naturalgas prior to its passage through the last one of said remainder of saidzones so that the beds of adsorbent material therein will be cooled;periodically shifting the relative positions of the particular adsorbentmaterial and the particular flow of fluid in each of said zones so thateach zone becomes, in succession, a reactivation zone, a purging zone, acooling zone, and a dehydration zone; continually directing the flow ofthe captaive gas as it is recycled and after its passage through thereactivation zone, through a condensing and separating zone and therecondensing and recovering the water and condensable hydrocarbonstherefrom; continuously diverting a portion of the stripped efliuent gasfrom the cooling zone for use as the purging medium and continuouslydirecting the flow of the eflluent gas from the purging zone into theflow of the recycling captive activation gas on its way to be heated.

2. In the removal of water vapor and condensable hydrocarbons from wetnatural gas involving the contact of adsorbent material with the gaswith resultant adsorption of the water vapor and condensablehydrocarbons by the adsorbent material and the subsequent treatment ofthe adsorbent material with a heated medium to vaporize and remove thewater and condensable hydrocarbons and thereby reactivate the adsorbentmaterial for further contact with the natural gas, the improvement whichcomprises maintaining at least one bed of adsorbent material in each ofa plurality of zones; continuously heating and recycling a flow ofcaptive gas through at least one of said zones to vaporize the water andcondensable hydrocarbons contained in the adsorbent material therein andreactivate the adsorbent material; continuously directing a first flowof a purging medium through at least another one of said zones to purgethe adsorbent material therein and the zone of other gas therein;continuously directing a second flow of a purging medium through atleast another one of said zones to after its passage through purge theadsorbent material therein and the zone of other gas therein; naturalgas through the remainder of said zones so that directing a continuousflow of the raw the water vapor and some of the condensable hydrocarboncontent of the natural gas will be adsorbed by the adsorbent materialtherein; continuously cooling the raw natural gas prior to its passagethrough the last one of said remainder of said zones so that the beds ofadsorbent material therein will be cooled; continuously directing theflow of the captive gas as it is recycled and the reactivation zone,through a condensing and separating zone and there condensing andrecovering the water and condensable hydrocarbons therefrom;periodically shifting the relative positions of the particular adsorbentmaterial and the particular flow of fluid in each of said zones so thateach zone becomes, in succession, a second purging zone, a reactivationzone, a first purging zone, a cooling zone, and a dehydration zone;continuously diverting a portion of the stripped efiluent gas from thecooling zone for use as the first purging medium and continuouslydirecting the flow of the eflluent gas from the first purging zone intothe flow of the recycling captive gas on its way to be heated;continuously diverting a portion of the captive reactivation gas fromits recycling path for use as the second purging medium; andcontinuously directing the flow of the eflluent gas from the secondpurging zone back into the flow of the raw gas being treated on its wayto be dehydrated.

3. In the removal of water vapor and condensable hydrocarbons from Wetnatural gas involving the contact of adsorbent material with the gaswith resultant adsorption of the water vapor and condensable hydracarbons by the adsorbent material and the subsequent treatment of theadsorbent material with a heated medium to vaporize and remove the waterand condensable hydrocarbons and thereby reactivate the adsorbent ma-.terial for further contact with the natural gas, the improvement whichcomprises maintaining at least one bed of adsorbent material in each ofa plurality of zones; continuously heating and recycling a flow ofcaptive gas through at least one of said zones to vaporize the water andcondensable hydrocarbons contained in the adsorbent material therein andreactivate the adsorbent material; continuously directing a first flowof a purging medium through at least another one of said zones to purgethe adsorbent material therein and the zone of other gas therein;continuously directing a second flow of a purging medium through atleast another one of said zones to purge the adsorbent material thereinand the zone of other gas therein; directing a continuous flow of theraw natural gas so that it will make a first passage through at least anadditional one of said zones and a second passage through the remainderof said zones so that the water vapor and some of the condensablehydrocarbon content of the natural gas will be adsorbed by the adsorbentmaterial therein; continuously cooling the raw natural gas prior to itspassage through the last one of said remainder of said zones so that thebeds of adsorbent material therein will be cooled; continuouslydirecting the flow of the captive gas as it is recycled and after itspassage through the reactivation zone, through a condensing andseparating zone and there condensing and recovering the water andcondensable hydrocarbons therefrom; periodically shifting the relativepositions of the particular adsorbent material and the particular flowof fluid in each of said zones so that each zone becomes, in succession,a second purging zone, a reactivation zone, a first purging zone, acooling zone, and a dehydration zone; continuously diverting a portionof the stripped effluent gas from the cooling zone for use as the firstpurging medium and continuously directing the flow of the efiiuent gasfrom the first purging zone into the flow of the recycling captive gason its way to be heated;

continuously diverting a portion of the captive reactiva-- tion gas fromits recycling path for use as the second purging medium; the eflluentgas from the second purging zone back into .ing its flow through the andcontinuously directing the flow of the flow of the raw gas being treatedon its way to be I dehydrated.

.carbons and thereby reactivate the adsorbent material for furthercontact with the natural gas, the improvement which comprises rotating aseries of separated thin beds of adsorbent material directly insuccession and substantially continuously relative to and through asecond purging stage, a reactivation stage, a'first purging stage, acooling stage, a third adsorption stage, a second adsorption stage, anda first adsorption stage; continuously directing a flow of the gas to betreated in succession through said first adsorption stage, said secondadsorption stage, said third adsorption stage, and said cooling stage;continuously cooling the gas being treated as it passes from said thirdadsorption stage to said cooling stage; continuously heating andrecycling a flow of activation gas through said reactivation stage tovaporize the water and condensable hydrocarbons contained in the beds ofadsorbent material therein and reactivate the beds; continuouslydirectingrthe flow of the captive gas as his recycled and after itspassage through the reactivation stage, through a condensing andseparating stage and there condensing and removing the water andcondensable hydrocarbons; continuously diverting a portion of the .fiowof the effluent gas from the cooling stage and directing its flowthrough the first purging stage to remove all of the activation gastherefrom and continuously directing the flow of the effiuent gas fromthe first purging stage into the recycling activation gas on its way tobe heated; continuously diverting a portion of the recycling activationgas on its way to be heated and directing its flow through the secondpurging stage to remove all of the raw natural gas therefrom; andcontinuously directing the flow of the eflluent gas from the secondpurging stage into the flow of the raw natural gas on its way to betreated.

5. The method as set forth in claim 4, including the step ofcontinuously adding inert gas to the recycling activation gas on its Wayto be heated.

6. In the removal of water vapor and condensable hydrocarbons from wetnatural gas involving the contact of adsorbent material with the gaswith resultant adsorption of the water vapor and condensablehydrocarbons by the adsorbent material and the subsequent treatment ofthe adsorbent material with a heated medium to vaporize and remove thewater and condensable hydrocarbons and thereby reactivate the adsorbentmaterial for further contact with the natural gas, the improvement whichcomprises rotating a series of separated thin beds of adsorbent materialdirectly in succession and substantially continuously relative to andthrough a second purg ing stage; a reactivation stage, a first purgingstage, and a succession of adsorption stages; continuously directing aflow of the gas to be treated in succession through said adsorptionstages; continuously heating and recycling a flow of activation gasthrough said reactivation stage to vaporize the water and condensablehydrocarbons contained in the beds of adsorbent material therein andreactivate the beds; continuously directing the flow of the captive gasas it is recycled and after its passage through the reactivation stage,through a condensing and separating stage and there condensing andremoving the water and condensable hydrocarbons; continuously divertinga portion of the flow of the efiiuent stripped gas from the last of saidadsorption stages and direct- -first purging stage to remove all of theactivation gas therefrom and continuously directing the flow of theeffluent gas from the first purging stage into the recycling activationgas on its Way to be heated; continuously diverting a portion of therecycling activation gas on its way to be heated and directing its flowthrough the second purging stage to remove all of the raw natural gastherefrom; and continuously directing the flow of the elfiuent gas fromthe second purging stage into the flow of the raw natural gas on its wayto be treated.

7. In the removal of Water vapor and condensable hydrocarbons from wetnatural gas involving the contact of adsorbent material with the gaswith resultant adsorption of the water vapor and condensablehydrocarbons by the adsorbent material and the subsequent treatment ofthe adsorbent material with a heated medium to vaporize and remove thewater and condensable hydrocarbons and thereby reactivate the adsorbentmaterial for further contact with the natural gas, the improvement whichcomprises rotating a series of separated thin beds of adsorbent materialdirectly in succession and substantially continuously relative to andthrough a second purging stage, a reactivation stage, a first purgingstage, and an adsorption stage; continuously directing a flow of the gasto be treated through said adsorption stage; continuously heating andrecycling a flow of activation gas through said reactivation stage tovaporize the water and condensable hydrocarbons contained in the beds ofadsorbent material therein and reactivate the beds; continuouslydirecting the flow of the captive gas as it is recycled and after itspassage through the reactivation stage, through a condensing andseparating stage and there condensing and removing the Water andcondensable hydrocarbons; continuously diverting a portion of the flowof the efiluent stripped gas from said adsorption stage and directingits flow through the first purging stage to remove all of the activationgas therefrom and continuously directing the flow of the effluent gasfrom the first purging stage into the recycling activation gas on itsway to be heated; continuously diverting a portion of the recyclingactivation gas on its Way to be heated and directing its flow throughthe second purging stage to remove all of the raw natural gas therefrom;and continuously directing the flow of the efiluent gas from the secondpurging stage into the flow of the raw natural gas on its way to betreated.

8. In the removal of water vapor and condensable hydrocarbons from wetnatural gas involving the contact of adsorbent material With the gaswith resultant adsorption of the Water vapor and condensablehydrocarbons by the adsorbent material and the subsequent treatment ofthe adsorbent material with a heated medium to vaporize and remove thewater and condensable hydrocarbons and thereby reactivate the adsorbentmaterial for further contact with the natural gas, the improvement whichcomprises rotating a series of separated thin'beds of adsorbent materialdirectly in succession and substantially continuously relative to andthrough a reactivation stage, a purging stage, a cooling stage, and asuccession of adsorption stages; continuously directing a flow of thegas to be treated in succession through said adsorption stages and saidcooling stage, continuously cooling the gas being treated as it passesfrom the last of said adsorption stages to said cooling stage;continuously heating and recycling a flow of activation gas through saidreactivation stage to vaporize the water-and condensable hydrocarbonscontained in the beds of adsorbent material therein and reactivate thebeds; continuously directing the flow of the captive gas as it isrecycled and after its passage through the reactivation stage, through acondensing and separating stage and there condensing and removing thewater and condensable hydrocarbons; continuously diverting a portion ofthe flow of the effluent stripped gas from said cooling stage anddirecting its flow through the purging stage to remove all of theactivation gas therefrom and continuously directing the flow of theeffluent gas from the purging stage into the recycling activation gas onits Way to be heated.

References Cited in the file of this patent UNITED STATES PATENTS1,721,033 Okachi July 16, 1929 1,872,783 Miller Aug. 23, 1932 1,998,774Bulkeley Apr. 23, 1935 2,053,159 Miller Sept. 1, 1936 2,507,608 MillerMay 16, 1950 2,535,902 Bailey Dec. 26, 1950 2,630,191 Miller Mar. 3,1953

1. IN THE REMOVAL OF WATER VAPOR CONDENSABLE HYDROCARBONS FROM WETNATURAL GAS INVOLVING THE CONTACT OF ADSORBENT MATERIAL WITH THE GASWITH RESULTANT ADSORPTION OF THE WATER VAPOR AND CONDENSABLEHYDROCARBONS BY THE ADSORBENT MATERIAL AND THE SUBSEQUENT TREATMENT OFTHE ADSORBENT MATERIAL WITH A HEATED MEDIUM TO VAPORIZE AND REMOVE THEWATER AND CONDENSABLE HYDROCARBONS AND THEREBY REACTIVATE THE ADSORBENTMATERIAL FOR FURTHER CONTACT WITH THE NATURAL GAS, THE IMPROVEMENT WHICHCOMPRISES MAINTAINING AT LEAST ONE BED OF ADSORBENT MATERIAL IN EACH OFA PLURALITY OF ZONES; CONTINUOUSLYY HEATING AND RECYCLING A FLOW OFCAPTIVE GAS THROUGH AT LEAST ONE OF SAID ZONES TO VAPORIZE THE WATER ANDCONDENSABLE HYDROCARBONS CONTAINED IN THE ADSORBENT MATERIAL THEREIN ANDREACTIVE THE ADSORBENT MATERIAL; CONTINUOUSLY DIRECTING THE FLOW OF APURGING MEDIUM THROUGH AT LEAST ANOTHER ONE OF SAID ZONES TO PURGE THEADSORBENT MATERIAL THEREIN BY REMOVING ALL OF THE REMAINING ACTIVATIONGAS, MOISTURE AND CONDENSABLE HYDROCARBONS THEREFROM; DIRECTING ACONTINUOUS FLOW OF THE RAW NATURAL GAS SO THAT IT WILL MAKE A FIRSTPASSAGE THROUGH AT LEAST AN ADDITIONAL ONE OF SAID ZONES AND A SECONDPASSAGE THROUGH THE REMAINDER OF SAID ZONES SO THAT THE WATER VAPOR ANDSOME OF THE CONDENSABLE HYDROCARBON CONTENT OF THE GAS WILL BE ADSORBEDBY THE ADSORBENT MATERIAL THEREIN; CONTINUOUSLY COOLING THE RAW NATURALGAS PRIOR TO ITS PASSAGE THROUGH THE LAST ONE OF SAID REMAINDER OF SAIDZONES SO THAT THE BEDS OF ADSORBENT MATERIAL THEREIN WILL BE COOLED;PERIODICALLY SHIFTING THE RELATIVE POSITIONS OF THE PARIN EACH OF SAIDZONES SO THAT EACH ZONE BECOMES, IN SUCCESSION, A REACTIVATION ZONE, APURGING ZONE, A COOLING ZONE, AND A DEHYDRATION ZONE; CONTINUALLYDIRECTING THE FLOW OF THE CAPTAIVE GAS AS IT IS RECYCLED AND AFTER ITSPASSAGE THROUGH THE REACTIVATION ZONE, THROUGH A CONDENSING ANDSEPARATING ZONE AND THERE CONDENSING AND RECOVERING THE WATER ANDCONDENSABLE HYDROCARBONS THEREFROM; CONTINUOUSLY DIVERTING A PORTION OFTHE STRIPPED EFFUENT GAS FROM THE COOLING ZONE FOR USE AS THE PURGINGMEDIUM AND CONTINUOUSLY DIRECTING THE FLOW OF THE EFFUENT GAS FROM THEPURGING ZONE INTO THE FLOW OF THE RECYCLING CAPTIVE ACTIVATION GAS ONITS WAY TO BE HEATED.